Control of nitrogen in ammonia synthesis



July 14, 1959 E. w. JORDAN ETAT CONTROL OF NITROGEN 1N AMMONIA SYNTHESIS Filed Jan. 2, 195,1

2 sheets-sheet 1 illu.) lran.

ATTORNEYS July 14, 1959 E. w. JORDAN ETAL 2,894,821

CONTROL 0F NITROGEN IN AMMONIA SYNTHESIS Filed Jan. 2, 1951 2 Sheets-Sheet 2 THERMAL CONDUCTlvlTY 6I) CELL 6o i l g RECORDER CONTROLLER F/G. Z

7l DIFFE RENTIAL FLow RECORDER CONTROLLER fg''* SEPARATION EURNACE 65 66- ZONE 67 INVENTOR. E.W. JORDAN W. R. PIERCE F/G. 4. y

#YMM ATTORNEYS United, States Paf-O f z,s94`,sz1

' CONTROL 0F NITROGEN 1N AMMONIA SYNTHESIS Earl W. Jordan, Dumas, Tex., and Weller R. Pierce,

Bartlesville, Okla., assignors to Phillips Petroleum Company, a corporation of Delaware 'Application January 2, 1951, Serial No. 203,868

' "11 claims. (cm3-19s) This invention relates 'to a continuous process for the controlof'` nitrogen content inamrnonia synthesis gas. In one of its more specific aspects it relates to a method whereby the nitrogen content of feed gas to an ammonia synthesis process is continuously controlled by regulation 1950, andy now abandoned.

In the process for manufacturing ammonia the rst step is usually that of producing a feed gas containing 3 parts 'of hydrogen for each part of nitrogen. This may be accomplished by reacting a hydrocarbon such as methane asmay b'e found in natural gas with superheated stealnin the presence of a suitable catalyst. This reaction generally takes place in what is known as the primary reformer. The eluent from this reaction comprising hydrogen, carbon monoxide, carbon dioxide, and methane, is passed to what is known as the secondary reformer to which s also added a suiiicient quantity of airl which, after the oxygen is removed in the form of oxygen containing compounds, provides the correct proportion of nitrogen. In the secondary reformer a portion ofthe hydrogen and carbon monoxide are oxidized with the oxygen in the air and this combined with the reformed methane provides a product containing steam, carbon dioxide, carbon monoxide, nitrogen, hydrogen, and methane. This material is then passed to a shift converter for conversion of most of the carbon monoxide to carbon dioxide. Suitable means are then used for removing the steamsuch as a water quench, the carbon dioxide such as amine scrubbing and the residual carbon monoxide suchas ycopper ammonium formate solution. Such treatment leaves a product gas containing primarily hydrogen and nitrogen although some methane and inert gases such as argon, helium, and so forth will also be present. This gas which is the feed for ammonia production is passed to an ammonia converter at an elevated pressure where it is converted in the presence of a suitable catalyst to ammonia.V l The eflluent gas from such conversion or synthesis as it is often called, is passed through suitable equipment for removal of ammonia such as conventional cooling and refrigerating equipment. After the removal of the ammonia, the remaining gas will still contain some hydrogen and nitrogen along with minor quantities of methane and the previously mentioned inert gases which are now ngreater proportions than in the feed gas because of the removal of some'of the hydrogen and nitrogen as ammonia. For economical reasons this gas must be recycled to utilize as much hydrogen and nitrogen as possible. It is evident that since the make-up feed gas to the ammonia synthesis step contains'a quantity of methane all the time, some means must be utilized for maintaining the methane content'of 2,894,821 Patented July 14, 1959 the cycle gas and concomitantly of the synthesis feed gas from building up beyond a desired amount. One reason for requiring this is that the ammonia conversion is considerably reduced when too great a quantity of methane is present, apparently due mainly to dilution of the hydrogen and nitrogen. The usual procedure is -to maintain the methane content of the feed gas to ammonia synthesis, including cycle gas, at a desired percentage by purging a portion of the cycle-gas.

It is evident that slight fluctuations in 'the ratio of natural gas to steam may take place in the primary reformer thus causing some variation in the quantity of hydrogen produced. Other causes of variation inthe hydrogen content will be the activity of the reforming catalyst used, the quantity of air supplied to the secondary reformer, space velocity, and reforming temperatures.

j After removalv of the water and carbon dioxidethegas For economical reasons it would be very desirable to maintain the ratio ofnitrogen to hydrogen at about 1 to 3 even though there may bev fluctuations in the quantities of hydrogen produced.

An object of this invention is to provide a feed gas to ammonia synthesis containing hydrogen and nitrogen in a ratio of 3 to l.

Another object of this invention is to provide a method for controlling the nitrogen content of feed. gas to ammonia synthesis.

Another object of this invention is to continuously control the ratio of hydrogen to nitrogen in feed gas to ammonia synthesis by controlling the amount of air introduced to the secondary reformer in relation tothevariation in ratio of hydrogen to nitrogen in the feed gas.

Another object ofgthisjinvention is to controlthe ratio of hydrogen to nitrogen'content of feed gas to ammonia synthesis by controlling the amount of air introducedto the secondary reformer in relation to the variation in ratio of hydrogen to nitrogen as determined in the cycle gas. Y

Still another object is to provide a continuous method for automatically determining the nitrogen content of cycle gas to ammonia synthesis and to controlthe air feed to the secondary reformer in relation to this quantity.

Other objects and advantages of our invention will be apparent to one skilled in the art from the following discussion and disclosure. y y p l We have discovered a very advantageous method for continuously controlling the overall ratio of nitrogen to hydrogen in the feed gas to ammonia synthesis by the determination of the hydrogen and/or nitrogen content or the hydrogen-nitrogen ratio of the cycle or feed gas, and by such determination controllingthe airfeed to theA secondary reformer which is the source of nitrogen.

In the practice of a preferred embodiment of our in-` vention, a portion of cycle gas, i.e., gas recycledfrom and back to ammonia synthesis of which the methane content is maintained constant as by Vpurging a portion of the stream when the methane content becomes too high, is continuously passed through a iiow controller whereby a constant volume of ow is maintained. This gas, which contains byth hydrogen vand nitrogen in addition to methane and inert gases, is passed to a copper oxide furnace which converts the hydrogen and methane to water and carbon dioxide, concomitantly reducing the copper oxide. The eluent from this reaction is then suitably treated to remove the water and carbon dioxide thus leaving a gas containing nitrogen and inert gases such as argon, helium, and the like. Other methods of oxidizing combustibles in the gas can be utilized, for example, a controlled amount' of air can bev used to burn combustibles in the gas and the combustion products removed as above. In such a case, allowance for nitrogen added in the oxidizing air must bev made.

' is passed through asuitable flow meter and then to 2,894,821 t v y treatment incontact with metallic calcium for removal of nitrogen as calcium nitride. SuitableV temperatures for this reaction are generally within the range of 700-750 C. In this manner nitrogen is removed from the gas stream leaving only the inert gases. These gases areV then passed through a second ilow meter and on to vent. Since a known volume of gas is withdrawn and this gas contains a known or fixed percentage of methane, this rst meter while measuring the nitrogen and inerts also gives a measurement of the hydrogen content of the said withdrawn gas. The second flow meter measures the differential across the calcium tube furnace which is a direct measure ofthe nitrogen content of the gas.

A multipoint dilterential llow recorder-controller can be utilized to take advantage of the determination of the nitrogen and hydrogen content of the sample gas andl to control the air inlet to the secondary reformer in response to adverse changes in the ratios of these, one to the other.

The recorder-controller is so adjusted, knowing the constant rate of ow of the sample stream at its origin and the constant methane content thereof, to record the ow of hydrogen which amounts to the initial ow of sample gas less the ilow after the removal of hydrogen and methane after adding the known constant quantity of methane present. Such adjustments may be made in known manner on conventional multipoint recordercontrollers.

The recorder-controller is also adjusted to record the differential in iiow across the calcium tube furnace as measured by the rst and second llow meters. The recorder-controller is then set so as to actuate the valve in the air line to the secondary reformer in response to changes in the ratio of hydrogen to nitrogen as measured by ow.

The following will exemplify the above discussed method for determining the hydrogen and nitrogen content of an ammonia synthesis feed gas. A controlled volume of gas comprising, say, 40 cubic centimeters per minute, is used. By previous analysis the methane content is 8 volume percent of the total gas or 3.2 cubic centimeters. The gas which is withdrawn continuously from the ammonia synthesis feed is passed through a copper oxide furnace under conditions which will cause all of the methane and hydrogen present to be converted to water andV carbon dioxide. After removal of these materials the gas is then passed through a flow meter of a conventional type which will read the reduction in gas ow from the constant volume originally started with and which shows that the ow of gas has been reduced by 27.2 cubic centimeter per minute. An alternative is to adjust this ow meter so that it automatically deducts the known quantity of methane from the volume of gas by which the flow was reduced thus causing the meter to read the hydrogen content directly. Conventional meters adapted from such adjustment as are known to those skilled in the art are used. When this alternative is not employed the reading of the flow meter is transmitted to a conventional differential recorder-controller which makes a similar adjustment and records directly the volume ofhydrogen. Following measurment of the gas for determination of the hydrogen present, it is contacted with metallic calcium at conditions which cause the nitrogen to react with the calcium to form calcium nitride thus removing the nitrogen from the gas. Measurement of the gas ow per minute is again made, and the differential between this Volume and that measured by the first flow meter, taking into consideration the cor'- rection for methane if the rst flow meter was adjusted to read hydrogen directly, is the volume of nitrogen present which is 8 cubic centimeters. The remaining gas, that which is directly measured by the second ow meter, comprises inerts such as argon and helium. In the present case this would amount to 4.8 cubic centimeters. By Comparison of theV ratio of hydrogen to nitrogen, the

amounts 'of which are determined as just discussed, with a desired ratio, the recorder-controller is made to actuate the valve in the air line to the secondary reformer when the ratios do not compare favorably. A diaphragm or solenoid valve of conventional design is used and is actuated either by changes in pressure of instrument air on the diaphragm of thel valve or variation in electrical impulse to the solenoid. By` the process above discussed, we not only maintain a more accurate and constant control of the nitrogen content of the ammonia synthesis feed gas, but eliminate the irregularities which wouldl obviously be present when attempting to make this control manually.

In another embodiment of our invention which is practiced in combination with the invention disclosed in copending application Serial No. 136,742, tiled January 4, 1950, now Patent No. 2,667,410, which teaches analyzing the methane content of the eluent from a primary reformer in an ammonia. synthesis processl andv by such analysis controlling both the feed gas to the reformerl and the gas to the heater for said reformer, a portion of the feed gas or make-up gas to the ammonia synthesis is withdrawn prior to introduction thereto of cycle gas. By operating in this manner the methane content of themake-up gas is known (changes in nitrogen and hydrogencontent will cause very slight change in the perv cent methane: so small that they may be disregarded) and more rapid changes in the ratio of feed gas components may be made without first waiting for the gas to pass through the ammonia synthesis reactor.

In another embodiment of our invention, the hydrogennitrogen ratio in an ammonia synthesis process is controlled by measuring the thermal conductivity of a portion of the cycle gas in a thermal conductivity cell. Since the methane content of the cycle gas is keptl constant as hereinbefore described, the variables in composition of the cycle gas are hydrogen and nitrogen-argon. Since nitrogen and argon are both added by air, they may be treated as one gas; thus the cycle gas may be co'nsidered as containing only two variables, i.e., hydrogeny and nitrogen-argon. The thermal conductivity of this two component system can be measured and the hydrogen-nitrogen ratio controlled by controlling the addition of air to the secondary reformer in response to changes in the thermal conductivity from a predetermined value. A recorder-controller of conventional type can be used to respond to the thermal conductivity changes as measured by the thermal conductivity cell and actuate a valve in the air line to the secondary reformer thereby maintaining the desired hydrogen-nitrogen ratio by varying the amount of air supplied to the secondary reformer.

In another embodiment `of our invention the hydrogennitrogen ratio can be controlled in an ammonia synthesis process of the type described above by employing a gravitometer of conventional design for measuring the density of the cycle gas. As pointed out above,l the cycle gas may be considered a two component system, i.e., hydrogen and nitrogen-argon, provided the methane content is maintained constant. component system can be measured by said gravitometer and the addition of air to the secondary reformer controlled in response to said measurement. A recorder controller can be used to respond to fthe changes in gravity lof the cycle gas as measured byr said gravitometer and operate a valve in the air line to the secondary reformer responsive to changes in the said measured gravity from a predetermined value so as to maintain the desired hydrogen-nitrogenk ratio.

In still another embodiment of our invention for the control of the hydrogen-nitrogen ratio in an ammonial synthesis process, a diiferential ow recorder-controller, with methane and hydrogen removed between the two orifices, can be used to control Vthe addition of yair to the secondary reformer and hence control the-hydrogennitrogen ratio in an ammonia synthesis process. As

The density of this twol noted above, the methane content ofthe cycle gas is maintained" constant and known, thus the volume of hydrogen removed can be, readily calculated by subtractingvr the known'volume of methanejom vthe total decrease in the cycle gas'whicl occurs inthe combustion tube'between the two orifices.' The methane and hydrogen are removed between the oric'es' by passing the cycle gas over copper oxide and employing suitable scrubbing as hereinbefore described. This measurment of the volume of hydrogencontained in the cycle gas can' be used by the differential flow recorder-controller to operate a valve in the air linev to the secondary reformer and thereby control the addition of air to the secondary reformer and hence'the hydrogen-nitrogen ratio in an ammonia synthesis process.

It will be apparent that the last 4three embodiments of our invention, while having the advantage of being simple and easy Vto operate, are not as accurate asfthepreferred embodiment. The embodiment to be used in any particular case will depend upon the accuracy of control necessary, and the impurities inthe charging gas.

A- more complete understanding of' some of the many aspelctsflof our'invention may be had by referring to Figure 1 of =the attached drawing, which is a schematic flow 1diagramof: said, 'preferredimodication of my invention, in conjunction with thel following discussion. Various additional valves, pumps, and other conventional equipment necessary for the' practiceof this invention will bef'arniliar to one skilled in the art andhave been omittedv from the drawing for the sake of clarity. vThe description provides one method of operatingour process; however, while this is representative in general of our process, various minor changes may be made in adapting it to 'the various conditions within the scope of the in`v vention. l

` Figure 2 isa schematic flow diagram of a modification of our invention wherein the hydrogen-nitrogen ratiok is controlled in an ammonia synthesis process by measuring the -thermal'conductivity of the cycle gas. The various reforming, conversion, separating, synthesis, recovery and methane analyzing vzones are the same as in Figure l and'thereforeare not shown as the function of themodifi'cation will be apparent to 'one skilledin theart upon reading of the discussion and examining the drawings herein shown.' -Fig'ure 3 is a schematic owdiagr'am of another modiiication of our invention wherein thehydrogen-nitrogen ratio in an ammonia synthesis process is controlled-'by measuring-the density 'of the cycle.' gas.' Again all'the steps in'fthe process are not vshown as 'they are the same as in Figurelgandrepeating' said 'steps is not Vnecessary as one skilled "ink the'art willund'erstand the function ofthe modification without such repetition. v f Figure 4 is Va'schematic vilo'vv diagram of still another modification of-ou1f inventionfwherein 'the hydrogennitrogen ratio in an ammonia synthesis process is controlled bya differential flow recorder-controller. Hydrogen and metlianeiare' 'removed between 4the Aorifices ofthe controller and the decrease in volume ofcycle gas, taking into'account thek known volume of methane removed, is usedfto control the air added to thereforming step and hence controlthe hydrogen-nitrogen ratio. Again all the steps in fthe processare not shown as'they'are ther same as Vin Figure 1 andv therefore f are not necessary in v an illustration of a modification of a method of controlling the hydrogen-nitrogen ratio in the process. `Refer nowto Figure 1 in the drawing, the discussion of which will also exemplify said preferred modification of our invention. Natural gas and superheated steam are passed through: lines '10` and'11.,rspecti v'e'ly, to primary .reforming zone' 12 `where they 'contact asuitable reforming catalyst such as supportedreduced nickel oxide at-,;a=temp`erature preferably in rthe range of 700-750 C g Theefuent from'. the fzone containing primarily hYdPQ81 1, carbon monoxide, and, carbon'y dioxide" alongy 6 i with a minor quantity of methane is passed through kline 13 to secondary reforming zone 14. In this zone the gas contacts another bed of reforming catalyst which may either be the same as that used in the primary reforming zone or diiferent. A suitable temperaturel for this reaction is in the range of 8501100 C. Intro* duced also to this zone is a stream of air passed through line 16 which provides the nitrogen to 4beused inthe ammonia synthesis. In the secondary reforming zone the oxygen from the air oxidizes some of the hydrogen and carbon monoxide so that the oxygen may be easily removed leaving the nitrogen while a portion of the methane is reformed. The efiiuent from zone 14 is now passed via line 17 to a carbon monoxide conversion zone 18. In this zone the gas is contacted with-.a catalyst such as iron oxide and as is used'v in conventional carbon monoxide to carbon dioxide conversion. By such treatment the carbon monoxide content of the reformed gases now containing nitrogen is reduced toabout 2.'5 to 5 volume percent. From conversion zone 18 the gases are passed to a separation zone 20 through line'19 where water and carbon dioxide are removed by `conventional means such as quenching and amine scrubbing 'as through line 21. The gas to be fed to ammonia synthesisnow contains primarily hydrogen and nitrogen with'only'minor quantitiesV of inert gases and methane'. 'I'his gas is passed through line `22 to ammonia conversion zone 23 where it contacts an iron oxide catalyst at a temperature in the range of 450-550" C. and a pressure in the range of 1500 to 15,000 pounds per square inch. Conversioni!! this zone is desirably maintained at atleast 1 ()l percent per pass and preferably in the range of 10'-20,percen't per pass. Products from synthesis zone 23 are passed through 1ine`24 to ammonia recovery zone 26,.' where suitable means are employed for condensing the am# moniav and causing its removal in this fmanner. The liquid ammonia from this zone is removedvia line '27.' The effluent gas is removed from ammonia 'recovery zone 26 through line 28 and recycled to synthesis zone 23 via line 2 2. A side stream of therecycled gas is passed through line 29- to methane analyzing zone 31 which may be of the type'disclosed in copending appli# cation, Se`ri al No."136,776, filed Januaryf4, 1950, now' abandoned, orv v'an infrared spectrc'pphotoxrleter. The methane content'is continuously determined, whichjdeterminationis used to control a purge ofthe cyclelgas'. The analyzing zone is so set up as tofcontrol thevalve in purge line 33' in such a manner that 'a portion of the cycle streani'is vented-to maintain the methane content within-a predetermined range., 'l Another portion of themake-up gas for the ammonia synthesis is withdrawnfrom line 28 through" 'li11"e 37 and is passed -through a suitable iiow` controller 38' and through linev 39to 'a copper oxide furnace 41. In another''modication wherein a methane analyzer is use d to control the methane content of the gas fromntheeformersfa sample 'stream for hydrogen and nitrogen 'analyses' may be withdrawn from line 22 upstream .of the recycle'inlt as through line 3 5. In the copper oxide 'furnace the hydrogen and methane contentof the cyclegasfis burned to" water and' carbon dioxide, oxygen beingsupplied by the copper oxide.l Suitable temperaturesV for this reaction are in the rangev of 600-900" C. Vand preferably in the range of 60G-700 C., the latter made possible by the presence of about 1 percent iron oxidein the copper oxide. The effluent gas from the copper oxide furnace is then passed to separation zone 43 vthrough line 42. In this zone the water and carbon dioxide4V are removed as by absorption. Line 44 leading from zo1ie43 typies outlets `for the absorbed materials. The waterproduc'e'd inthe copperY oxide furnace may be removed by ab'sor'p tionginsilica gel or 'calcium chloride or-by condensation while the ycarbonv dioxide rnay be removed fby means'l of aqueouscausticor aminel The ga's nowcontainin'giolfy nitrogen and inerts such asargon andiheliumf'i'spassd from zone l43 through line 46 to a flow measuring zone 47 and v'from there through line 48 to a calcium tube furnace .49. ln this furnace the nitrogen in the gas is reacted'with metallic calcium at a temperature in the rangeof 700750 C. and at a sufficient flow rate and contact time that calcium nitride is formed. In this manner nitrogen in the gas is consumed and removed therefrom leaving inert gases. These gases are passed from furnace 49 through line 51 to a second flow measuring zone 52 and from there to vent as by line 53. By determination of the hydrogen content of the gas by the differential in flow across the flow controller 38 and the ilow measuring zone 47 less the known volume of methane, and by determination of the nitrogen content of the gas by the differential in ow across metallic calcium furnace thev lratio of hydrogen to nitrogen in the cycle gas Vmay be constantly known. These data are then used'for making changes inthe rate of introduction of air tothe secondary reformer, thus varying the ratio of hydrogen to nitrogen in the feed gas to ammonia synthesis. VIn a preferred embodiment of our invention a differential ilow recorder-controller .56 is connected with ow measuring zones 47 and 52 and automatically records the differential in ow across the ilow controller 38 and the ilow measuring zone 47 and across the calcium tube furnace. These differentials and the hydrogen to nitrogen ratio determined therefrom are then used to control the valve 54 in line 16 so as to maintain a very uniform ratio nitrogen to hydrogen in the ammonia conversion feed gas.

Referring now to Figure 2. A portion of the cycle gas is withdrawn through line 37 and passed through thermal conduetivitycell 60 and vented through vent 61. The thermal conductivity of theV cycle gas is measured in cell 60. The operation of such a cell is known to those skilled in the art. For example, a suitable cell includes a Zone, containing an electrical heating element, through which the gas mixture is passed whose thermal conduct-ivity is to Ibe measured. A Wheatstone bridge is connected lacross the heating element in this zone and a heating element in a similar zone which contains a standard or reference gas such as air. As the thermal conductivity of themeasured :gas mixture increases, an increased amount of heat is conducted away from the heating elementin the ymeasuring zone and the temperature of that heating element decreases. As the temperature of the heating element decreases, the resistance of the measurheating element decreases as compared to the standard or reference heating element. This decrease in resistance, which indicates anincrease iu thermal conductivity of the measured gas, is detected by'the Wheatstone bridge connecting the two heating elements. If the thermal conductivity of the gas mixture decreases, less heat will beconducted away from the measuring heating element and the temperature of the heating element increases. An increased temperature of the measuring heating element increases the resistance of the measuring heating element with respect to the standard or reference heating element which indicates a decrease in thermal conductivity of the measured gas. The increased resistance of the v'measuring heating element with respect to the standard or reference heating element is detected by the Wheatstone bridge connecting the two heating elements. The changes in thermal conductivity of a gas mixture as detected by a Wheatstone bridge in the manner just described can be utilized to control the addition ofnitrogenv to an ammonia synthesis process so as to maintain the hydrogen-nitrogen ratio at the dired value. `Aswas noted above, the lmethane content of the cycle gas is lconstant and since Iboth nitrogen and argon are added` by air, the cycle `gas may be considered as a two component system comprising hydrogen and nitrogenargon. Changesin the thermal conductivity of :the cycle ganasmeasured Iby cell 60, actuates recorder-controller Recorder-controller 68operatesY valve 54 in air line 16 in response to changes in thermal conductivity of the cycle gas, as measured by cell 60, and thereby regulates the addition of air to the secondary reformer 14 so as to maintain the desired hydrogen-nitrogen ratio in the process. The thermal conductivity of hydrogen is approximately nine times that of the nitrogen-argon component. Therefore if the thermal conductivity of the cycle `gas increases, too much hydrogen is present in the cycle gas and the controller 68 operates valve 54 so as to allow more air to enter reformer 14 and return the-hydrogen-nitrogen ratio to the desired value. Likewise, if the thermal conductivity of the cycle gas decreases, there is an excess of the nitrogen-argon component in the cycle gas, and controller 68 operates valve 54 so as to reduce the supply of air to reformer 14 and thereby return the hydrogen-nitrogen ratio to the desired value.

Referring now to Figure 3. A portion of the cycle gas in an ammonia synthesis process is passedthrough line 37 into gravitometer 62 and vented through vent v63. Gravitometer 62 measures the lgravity of the cycle gas. As was noted before, since the methane content of the cycle gas is kept constant and since nitrogen andargon are both added by air, the cycle gas may be considered a two component system comprising hydrogen .and nitrogen-argon. Recorder-controller 69 operates valve 54 in air line 16 in response to changes in gravity of the cycle gas as measured by gravitometer 62 and thereby regulates the amount of air supplied to reformer 14. lThe specific gravity of the nitrogen-argon component of the cycle gas is approximately 14 times that of hydrogen. Therefore if the specific gravity of the cycle gas increases, there is an excess of the nitrogen-argon cornponent and recorder-controller 69 operates valve 54 in air line 16 so as to reduce the amount of air supplied to reformer 14 thereby returning the hydrogen-nitrogen ratio to the desired value. Likewise, if the specific gravity of the cycle gas decreases, there is too much hydrogen in the cycle gas and controller 69 will operate valve 54 in air line 16 so as to increase the amount of air supplied to reformer 14 thereby returning the hydrogen-nitrogen ratio to the desired value.

Referring now to Figure 4. A portion of .the cycle Igas in an ammonia synthesis process is withdrawn in tube 37 and passed through orifice 64 into copper oxide furnace 65 and separation zone 66, then through orice 67 and vented through vent 70. Methane and hydrogen are removed between orifices 64 and 67 in furnace 65 and separation zone 66 by methods hereinbefore 'described. The decrease in Volume of the cycle gas between oriices 64 and 67 is measured by differential ow recorder-controller 71. Since the methane content of the cycle gas is held constant, the volume of the hydrogen present in the cycle gas can be readily determined by subtracting the known volume of methane in the cycle gas from the decrease in volume of the cycle gas between orifices 64 and 67. This volume of hydrogen in the cycle gas can be used to regulate the amount of air supplied to reformer 14 and thereby control the hydrogen-nitrogen ratio in the ammonia synthesis process. If the volume of the hydrogen in lthe cycle gas increases, as measured by differential ow recorder-controller 71, controller 71 operates valve 54 in air line 16 so as to increase the amount of airsupplied to reformer 14 aud return the hydrogen-nitrogen ratio to the desired value. Likewise Vif the volume of the hydrogen'in the cycle gas decreases, controller 71 opera-tes valve 54 in air line 16 so 'as to decrease the amount of air supplied to `reformer 14 and thereby return the'hydrogen-niu-ogen ratio to the desired value.

It is within the scope of our invention to withdraw the portion of the cycle gas used to control the hydrogennitrogen ratio in each modification of our invention either continuously or intermittently. Also lthe control devices of the various modifications of ourrinventiomif operated. intermittently, can be used to control hydrogennitrogen'ratios in several processes which are going on simultaneously.

Our invention is equally applicablev to other processes for manufacturing ammonia such as from blue ygas (compraising carbon monoxide and hydrogen) and blow gas (comprising carbon monoxide, carbon dioxide, and nitrogen) produced by the steam and air treatment of coke. In such a process our controller would regulate the portion of .blow gas, 'containingl the nitrogen for the ammonia, introduced to the blue gas, containing the hydrogen, in response to the hydrogen and nitrogen content of the ammonia synthesis gas.

lLikewise, ammonia may be synthesized from electroly-tic hydrogen to whichA is added a controlled quantity of air to supply the desired'amount of nitrogen. In this type of process the control would be of the inlet air in responseto the hydrogen-nitrogen ratio in the ammonia synthesisgas'. e

`AlthoughA this invention has been described in terms of its kpreferred vmodifications it is understood that various changes may be made without departing from the spirit or scope of the disclosure and theclaims.

I claim:

' l. In a process wherein a snythesis gas comprising nitrogen and hydrogenkin akpredetermined ratio is fed to an ammonia synthesis zone and wherein said synthesis gas is prepared by reforming a methane containing -gas with steam, introducing nitrogen and oxygen-containing .gas to the reformation product thereby oxidizing a Iportion of said products and supplying nitrogen, removing the resulting oxidized products, passing the thus prepared gas to said ammonia synthesis zone, removing the resulting ammonia and recycling the unconverted gas, the improvement comprising continuously withdrawing a controlled volume of gas from the recycling converted gas, continuously metering the methane content of the withdrawn stream, venting a portion of said recycling unconverted gas responsive to changes in the metered methane content from a predetermined value so as to maintain the methane content of the recycling gas constant, withdrawing a second stream of gas subsequent to the preparation of the synthesis gas having a known methane content so as to provide a controlled volume thereof, continuously removing the combustible from said stream of gas, continuously metering the ow of the resulting stream of gas in terms of decreased flow from said second controlled volume withdrawn, removing nitrogen from last said resulting stream, metering the flow of gas after nitrogen removal in terms of the difference in ow before and after nitrogen removal, metering the ratio of the two differences and adjusting said oxygen-containing gas input responsive to changes in the ratio of said differences to maintain a constant nitrogen to hydrogen ratio in said synthesis gas.

2. The improvement of claim l wherein the second said controlled volume of gas is withdrawn prior to introducing the gas to the ammonia synthesis zone.

3. The improvement of claim l wherein the second said controlled volume of gas is withdrawn from said recycle gas.

4. In a process wherein a synthesis gas comprising nitrogen and hydrogen in a predetermined ratio is fed to an ammonia synthesis zone and wherein said synthesis gas is prepared by reforming a methane-containing gas with steam, introducing nitrogen and oxygen-containing gas to the reformation product thereby oxidizing a portion of said products and supplying nitrogen, removing the resulting oxidized products, passing the thus prepared gas to said ammonia synthesis zone, removing the resulting ammonia and recycling the unconverted gas, the improvement comprising continuously withdrawing a stream of the recycle gas at a predetermined constant rate to provide a controlled volume, continuously metering the methane content of the withdrawn stream, venting a portion of said recycle unconverted gas responsive to changes in the metered methane content from a predetermined value so v as to maintain said methane content in said recycle gas constant, continuously withdrawing a second stream of said recycle gas having a known methane content so as to provide a controlled volume thereof, passing the said second withdrawn stream through a thermal conductivity cell, continuously determining the thermal conductivity of said stream, and adjusting said oxygen-containing gas introduction responsive to changes in said conductivity from a predetermined value so as to maintain a constant hydrogen-nitrogen ratio in said synthesis gas.

5. In a process wherein la synthesis gas comprising nitrogen and'hydrogen in a predetermined ratio is fed to an ammonia synthesis zone and wherein said synthesis gas is prepared by reforming a methane-containing gas with steam, introducing nitrogen and oxygen-containing gas to the reformation product thereby oxidizing a portion of said products and supplying nitrogen, removing the resulting oxidized product, passing the thus prepared gas to said arrmionia synthesis zone, removing the resulting ammonia and recycling the unconverted gas, the improvement comprising continuously withdrawing a stream of the recycle gas at a predetermined constant rate to provide a controlled volume, continuously metering the methane content of the withdrawn stream, venting a portion of said recycle unconverted gas responsive to changes in the metered methane content from a predetermined value sov as to maintain said methane content in said recycle gas constant, continuously withdrawing a second stream of said recycle gas having a known methane content so as to provide av controlled volume thereof, passing the said second withdrawn stream to a gravity cell continuously determining the gravity of said gas in said cell and adjusting said oxygen-containing gas introduced responsive to changes in said gravity from a predetermined value of each to maintain a constant hydrogen nitrogen ratio in said synthesis gas.

6. In a process wherein a synthesis gas comprising nitrogen and hydrogen in a predetermined ratio is fed to an ammonia synthesis zone and wherein said synthesis gas is prepared by reforming a methane-containing gas with steam, introducing air to the reformation product thereby oxidizing a portion of said products and supplying nitrogen, removing the resulting oxidized products, passing the thus prepared gas to said ammonia synthesis zone, removing the resulting ammonia and recycling the unconverted gas the improvement comprising, continuously withdrawing a stream of the recycle gas at a predetermined constant rate to provide a controlled volume, cont'muously metering the methane content of the withdrawn stream, venting a portion of said recycle unconverted gas responsive to changes in the metered content from a predetermined value so as to maintain said methane content of said recycle gas constant continuously withdrawing a second controlled volume of recycle gas removing combustible products from last said Withdrawn gas, metering the resulting ow in terms of ratio of said ow to said controlled volume, and adjusting the air introduction responsive to changes in said ratio to maintain a constant nitrogen to hydrogen ratio.

7. In a process wherein a synthesis gas comprising nitrogen and hydrogen in a predetermined ratio is fed to an ammonia synthesis zone and wherein said synthesis gas is prepared by reforming a methane containing gas with steam, introducing air to the reformation product thereby oxidizing a portion of said product and supplying nitrogen, removing the resulting oxidized product, passing the thus prepared gas to said ammonia synthesis zone removing the resulting ammonia and recycling the unconverted gas, the improvement comprising continuously withdrawing the stream of the recycled gas at a predetermined constant rate to provide a controlled volume, continuously metering the methane content of the withdrawn stream, venting a portion of said recycled unconverted gas responsive to changes in the metered methane content from the predetermined value so as to maintain said methane content in said recycled gas constant, withdrawing a second stream of recycled gas at a rate to maintain said second stream constant, oxidizing last said withdrawn gas thereby converting combustibles to carbon dioxide and water, removing resultant carbon dioxide and water, metering the flow of the resulting gas stream in terms of decreased ow from said control volume withdrawn, removing nitrogen from last said stream, metering the flow of gas after nitrogen removal in terms of the diierence in ilow before and after nitrogen removal, metering the ratio of the two diierences and adjusting said air input responsive to changes in the ratio of said differences to maintain a constant nitrogen to hydrogen ratio in said synthesis gas.

8. The improvement of claim 7 wherein the combustibles of the control withdrawn volume of gas is oxidized with copper oxide in the temperature range of 600900 C. and nitrogen is removed by contacting the nitrogencontaining gas with metallic calcium at a temperature in the range of 700-750" C. so .as to form calcium nitride.

9. A process for supplying a feed gas of predetermined hydrogen-nitrogen ratio to a reaction zone, said process comprising introducing a control volume of nitrogencontaining gas to a stream of hydrogen-containing gas removing free and combined oxygen gas from said stream, passing the resulting stream to said reaction zone, continuously withdrawing a controlled volume of gas of known methane content from said reactionrzone, oxidizing combustibles in said withdrawn gas. metering the ow of the resultant stream in terms of the difference in ow between the control volume and 'the resulting stream, removing nitrogen from the last resulting stream, metering the resulting diierence in ow and adjusting the nitrogen-containing gas input responsive to changes in the 12 ratio of the said'two differences to maintain said hydrogen-nitrogen ratio substantially constant.

10. The process of claim 9 wherein the nitrogen gas is air.

11. The proces of claim 9 wherein the nitrogen-containing gas is blow gas comprising carbon monoxide, carbon dioxide, and nitrogen.

References Cited in the iile of this patent UNITED STATES PATENTS OTHER REFERENCES Comprehensive Treatise on VInorganic and Theoretical Chemistry, Longmans, Green and Co., N.Y., 1928, vo1. 8, page 97 (Mellor).

Lunge: Technical Gas Analysis, D. Van Nostrand Co., N.Y., 1914, Vpage 1728.

lEckman: Industrial Instrumentation, John Wiley and Sons, NLY., 1950, page 184.

Chemical and YMetallurgical Engineering, May 1943, Report on Measurement and Control of Process Variables, pages 97-145. 

1. IN A PROCESS WHEREIN A SNYTHESIS GAS COMPRISING NITROGEN AND HYDROGEN IN A PREDETERMINED RATIO IS FED TO AN AMMONIA SYNTHESIS ZONE AND WHEREIN SAID SYNTHESIS GAS IS PREPARED BY REFORMING A METHANE CONTAINING GAS WITH STEAM, INTRODUCING NITROGEN AND OXYGEN-CONTAINING GAS TO THE REFORMATION PRODUCT THEREBY OXIDIZING A PORTION OF SAID PRODUCTS AND SUPPLYING NITROGEN, REMOVING THE RESULTING OXIDIZED PRODUCTS, PASSING THE THUS PREPARED GAS TO SAID AMMONIA SYNTHESIS ZONE, REMOVING THE RESULTING AMMONIA AND RECYCLING THE UNCOVERTED GAS, THE IMPROVEMENT COMPRISING CONTINUOUSLY WITHDRAWING A CONTROLLED VOLUME OF GAS FROM THE RECYCLING CONVERTED GAS, CONTINOUSLY METERING THE METHANE CONTENT OF THE WITHDRAWN STREAM, VENTING A PROTION OF SAID RECYCLING UNCOVERTED GAS RESPONSIVE TO CHANGES IN THE METERED METHANE CONTENT FROM A PREDETERMINED VALUE SO AS TO MAINTAIN THE METHANE CONTENT OF THE RECYCLING GAS CONSTANT, WITHDRAWING A SECOND STREAM OF GAS SUBSEQUENT TO THE PREPARATION OF THE SYNTHESIS GAS HAVING A KNOWN METHANE CONTENT SO AS TO PROVIDE A CONTROLLED VOLUME THEREOF, CONTINUOUSLY REMOVING THE COMBUSTIBLE FROM SAID STREAM OF GAS, CONTINUOUSLY METERING THE FLOW OF THE RESULTING STREAM OF GAS IN TERMS OF DECREASED FLOW FROM SAID SECOND CONTORLLED VOLUME WITHDRAWN, REMOVING NITROGEN FROM LAST SAID RESULTING STREAM, METERING THE FLOW OF GAS AFTER NITROGEN REMOVAL IN TERMS OF THE DIFFERENCE IN FLOW BEFORE AND AFTER NITORGEN REMOVAL, METERING THE RATIO OF THE TWO DIFFERENCES AND ADJUSTING SAID OXYGEN-CONTAINING GAS NPUT RESPONSIVE TO CHARGES IN THE RATIO OF SAID DIFFERENCES TO MAINTAIN A CONSTANT NITROGEN TO HYDROGEN RATIO IN SAID SYNTHESIS GAS. 